EP2007927A2 - Amalgam decomposer for mercury cathode cells for alkali chloride electrolysis - Google Patents

Amalgam decomposer for mercury cathode cells for alkali chloride electrolysis

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Publication number
EP2007927A2
EP2007927A2 EP07728030A EP07728030A EP2007927A2 EP 2007927 A2 EP2007927 A2 EP 2007927A2 EP 07728030 A EP07728030 A EP 07728030A EP 07728030 A EP07728030 A EP 07728030A EP 2007927 A2 EP2007927 A2 EP 2007927A2
Authority
EP
European Patent Office
Prior art keywords
amalgam
decomposer
rings
catalytic coating
amalgam decomposer
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Granted
Application number
EP07728030A
Other languages
German (de)
French (fr)
Other versions
EP2007927B1 (en
Inventor
Giovanni Meneghini
Raffaello Bertin
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Industrie de Nora SpA
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Industrie de Nora SpA
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Filing date
Publication date
Application filed by Industrie de Nora SpA filed Critical Industrie de Nora SpA
Priority to PL07728030T priority Critical patent/PL2007927T3/en
Publication of EP2007927A2 publication Critical patent/EP2007927A2/en
Application granted granted Critical
Publication of EP2007927B1 publication Critical patent/EP2007927B1/en
Not-in-force legal-status Critical Current
Anticipated expiration legal-status Critical

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    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B1/00—Electrolytic production of inorganic compounds or non-metals
    • C25B1/01—Products
    • C25B1/34—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis
    • C25B1/36—Simultaneous production of alkali metal hydroxides and chlorine, oxyacids or salts of chlorine, e.g. by chlor-alkali electrolysis in mercury cathode cells
    • C25B1/42—Decomposition of amalgams
    • C25B1/44—Decomposition of amalgams with the aid of catalysts
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/30—Loose or shaped packing elements, e.g. Raschig rings or Berl saddles, for pouring into the apparatus for mass or heat transfer
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/20—Carbon compounds
    • B01J27/22—Carbides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/02—Impregnation, coating or precipitation
    • B01J37/0215—Coating
    • B01J37/0225—Coating of metal substrates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/34—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation
    • B01J37/349—Irradiation by, or application of, electric, magnetic or wave energy, e.g. ultrasonic waves ; Ionic sputtering; Flame or plasma spraying; Particle radiation making use of flames, plasmas or lasers
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/02—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds
    • B01J8/0242—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical
    • B01J8/025—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with stationary particles, e.g. in fixed beds the fluid flow within the bed being predominantly vertical in a cylindrical shaped bed
    • C—CHEMISTRY; METALLURGY
    • C25—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES; APPARATUS THEREFOR
    • C25B—ELECTROLYTIC OR ELECTROPHORETIC PROCESSES FOR THE PRODUCTION OF COMPOUNDS OR NON-METALS; APPARATUS THEREFOR
    • C25B9/00—Cells or assemblies of cells; Constructional parts of cells; Assemblies of constructional parts, e.g. electrode-diaphragm assemblies; Process-related cell features
    • C25B9/005—Amalgam decomposition cells
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/00796—Details of the reactor or of the particulate material
    • B01J2208/00884—Means for supporting the bed of particles, e.g. grids, bars, perforated plates
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2208/00—Processes carried out in the presence of solid particles; Reactors therefor
    • B01J2208/02—Processes carried out in the presence of solid particles; Reactors therefor with stationary particles
    • B01J2208/023—Details
    • B01J2208/024—Particulate material
    • B01J2208/025—Two or more types of catalyst
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/302—Basic shape of the elements
    • B01J2219/30215—Toroid or ring
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/302—Basic shape of the elements
    • B01J2219/30223—Cylinder
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30408—Metal
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/304—Composition or microstructure of the elements
    • B01J2219/30475—Composition or microstructure of the elements comprising catalytically active material
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/30—Details relating to random packing elements
    • B01J2219/318—Manufacturing aspects
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J27/00—Catalysts comprising the elements or compounds of halogens, sulfur, selenium, tellurium, phosphorus or nitrogen; Catalysts comprising carbon compounds
    • B01J27/20—Carbon compounds
    • B01J27/22—Carbides
    • B01J27/224—Silicon carbide
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B11/00—Obtaining noble metals
    • C22B11/10—Obtaining noble metals by amalgamating
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B3/00—Extraction of metal compounds from ores or concentrates by wet processes
    • C22B3/20—Treatment or purification of solutions, e.g. obtained by leaching
    • C22B3/22—Treatment or purification of solutions, e.g. obtained by leaching by physical processes, e.g. by filtration, by magnetic means, or by thermal decomposition
    • C—CHEMISTRY; METALLURGY
    • C22—METALLURGY; FERROUS OR NON-FERROUS ALLOYS; TREATMENT OF ALLOYS OR NON-FERROUS METALS
    • C22B—PRODUCTION AND REFINING OF METALS; PRETREATMENT OF RAW MATERIALS
    • C22B43/00—Obtaining mercury
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P10/00—Technologies related to metal processing
    • Y02P10/20—Recycling

Definitions

  • the production of chlorine by electrolysis of alkali chloride solutions is currently carried out by means of three different processes, namely the ion-exchange membrane, the porous diaphragm and the mercury cathode one.
  • the invention equally applies to the electrolysis of other alkali chlorides such as lithium or potassium chloride.
  • the mercury cathode-type electrolysis of sodium chloride solutions (brine in the following), based on a long-known technology, has experienced a continuous improvement in the cell structure (Ullmann's Encyclopaedia of Industrial Chemistry, VCH, Vol. A6, pag. 416) essentially directed to the decrease in the electric energy consumption and to the abatement of mercury emissions to the environment.
  • the problem of energy consumption reduction was tackled with success by replacing the original graphite anodes with titanium anodes provided with a catalytic coating based on oxides of platinum group metals, particularly effective for chlorine evolution.
  • the activated titanium anodes are also characterised by a long operative lifetime which allowed to substantially reduce the amount of cell shut-downs, quite frequent in the case of the corrodible graphite anodes: since maintenance shut- downs are critical for mercury emissions, the benefit obtained from this standpoint is apparent.
  • the sodium amalgam is fed to the upper portion of an amalgam decomposer shaped as a generally vertical vessel containing a filling of graphite fragments activated with a catalyst, for instance molybdenum oxide.
  • a catalyst for instance molybdenum oxide.
  • the amalgam flowing down the interstices between the graphite particles meets a countercurrent deionised water flow fed to the lower portion of the amalgam decomposer.
  • the catalytic action of graphite allows the amalgam decomposition reaction to proceed at an acceptable rate, with formation of caustic soda, which together with chlorine is the product of commercial interest, according to the following scheme:
  • amalgam droplet anodic area: Na(Hg) x ⁇ Na + + x Hg + e graphite particle (cathodic area): H 2 O + e ⁇ Y 2 H 2 + OH "
  • any single particle of catalytic material should comprise one or more pairs of separate anodic and cathodic microscopic areas, the anodic ones being wettable by the amalgam and the cathodic ones being non wettable and in intimate contact with the water flow. It would be further necessary to minimise the electrical resistance between the two types of area to provide the lesser hindrance to the electrons flowing from the anodic areas, where they are released by sodium ionisation, to the cathodic areas where they are consumed in the hydrogen evolution reaction.
  • the graphite particles undergo some grinding under the erosive action of the evolved hydrogen: as a first consequence, the filling undergoes a volume contraction in time that, once a value of about 20% is reached, leads to an intolerable productive capacity loss forcing the operators to discontinue the operation and to proceed with loading fresh catalyst.
  • the present invention has the purpose of overcoming the drawbacks of the prior art, in particular by providing a novel filling for amalgam decomposers operating in association with mercury cathode-type alkali chloride electrolysis cells. DESCRIPTION OF THE INVENTION
  • the invention relates to a catalyst consisting of amalgam- wettable metallic elements, whose surface is partially provided with a non-wettable catalytic coating, usable as filler for amalgam decomposers.
  • the elements of the invention are preferably cylindrical rings and the relevant surface partially or completely provided with a non-wettable catalytic coating is the external surface.
  • the amalgam-wettable metal may be advantageously selected from the group of iron, nickel, carbon steel, stainless steel, however one skilled in the art will also be capable of selecting additional metallic materials with suitable characteristics; according to one preferred embodiment of the invention, the catalytic coating consists of one or more metal carbides selected from the group of titanium, zirconium, niobium, tantalum, tungsten.
  • the application of the catalytic coating to the surface of the metallic elements may be advantageously carried out by spraying techniques, such as flame or plasma- spraying of powders;
  • the externally coated rings may be manufactured for example by applying the coating through micronised powder spraying on tubes and subsequently sectioning the tubes into rings.
  • the rings having an external surface partially provided with a catalytic coating may also be manufactured by assembling a multiplicity of tubes in a planar compact structure, applying the catalytic coating by micronised powder spraying on the two major surfaces of the structure and subsequently cutting the structure into rings wherein two lateral stripes of the external surface remain free of catalytic coating.
  • - fig. 2 sketch of the amalgam decomposer of fig. 1 with a partial internal side- view of the filling consisting of catalytically coated cylindrical rings, with a detail showing the structure of a preferred ring embodiment
  • the sketch of fig. 1 represents a longitudinal section of a mercury cathode electrolysis cell with the relevant amalgam decomposer, wherein 1 identifies the cell as a whole, 2 the cell body with the level 3 of brine and with the film 4 of mercury flowing on the carbon steel bottom, 5 the inlet end-box with the outlets 6 and 7 respectively for brine and disamalgamated mercury, 8 the inlet end-box with the outlets 9 and 10 respectively for the depleted brine and for the amalgam generated in the cell, 11 the anodes consisting of a planar structure of titanium rods coated with a catalytic coating for chlorine evolution based on platinum group metal oxides as known in the art, 12 the product chlorine outlet, 13 the amalgam decomposer provided with inlets for the amalgam coming from outlet 10 and for demineralised water 14, and with outlets for caustic soda 15 and hydrogen 16.
  • the anodes and the carbon steel bottom are connected respectively to the positive and to the negative pole of a rectifier (not shown in the figure).
  • Brine is partially converted to chlorine on the anodes and to sodium amalgam on the mercury mobile film.
  • the depleted brine exiting from 9 is delivered to the dechlorination, resaturation and purification units.
  • the chlorine withdrawn through nozzle 12 is cooled down, dried and pressurised before the direct appliance in user plants or before being liquefied and commercialised.
  • the amalgam produced in cell 1 is decomposed in the amalgam decomposer 13 in which it is put in contact with demineralised water in the catalytic filling 17: the reaction produces concentrated caustic soda, hydrogen and mercury which is recycled to the cell at 7.
  • the filling 17 consists of graphite particles activated with metal oxides, for instance molybdenum oxide.
  • amalgam decomposer is a cylindrical vessel of about 1100 mm diameter and overall height of 2100 mm, whereof about 1200 mm are occupied by the filling.
  • the inventors have surprisingly found that the inconveniences of the prior art, consisting of the poor catalytic activity of graphite, the consequent over-sizing of the amalgam decomposer and the insufficient operative lifetime, may be overcome by the introduction of fillings comprising a multiplicity of amalgam-wettable metal elements characterised by having their surface partially coated with a catalytic non amalgam-wettable coating for hydrogen evolution.
  • elements is herein intended to mean portions of metal of various geometrical shapes, dimensioned in order to provide, once stacked to form the filling, an extended contact surface for the reaction between amalgam and water.
  • This object is common to many chemical processes, such as for example the gas absorption in liquid phases or conversely the gas stripping from liquid phases: for such processes, very effective fillings were developed, consisting of a stack of single elements for instance in form of cylindrical rings, cylindrical semi-rings or Raschig rings.
  • the inventors have verified that all of these elements may be advantageously selected for the filling 17: in particular, it was found that the a particularly suitable filling, not only in terms of amalgam decomposition efficiency but also of cost and facility of coating application consists of cylindrical rings with an internal diameter of 10 - 40 mm, thickness of about 1 mm and length comprised between 10 and 40 mm.
  • Fig. 2 shows a more detailed sketch of the amalgam decomposer 13 according to an embodiment of the invention, wherein filling 17 is formed by a stack of cylindrical rings 19 supported by a grid 20.
  • the filling further comprises an element for homogenising the amalgam feed, for instance consisting of a perforated plate 21 also contributing to maintain the rings in position preventing harmful vibrations which could be caused by the evolution of hydrogen.
  • the amalgam entering from nozzle 22, flows in form of droplets 23 through cylindrical rings 19 in continuous contact with the surfaces thereof.
  • a flow of demineralised water 24 flows countercurrently towards the upper part of the amalgam decomposer, fed through nozzle 25: the water reacts with the amalgam by aid of the catalytic action of rings 19.
  • the structure of a preferred ring embodiment is shown in detail also in fig. 2: the ring 19 has an external surface partially provided with a catalytic coating 26 and an internal surface free of coating 27.
  • the metal of the rings 19 is wettable by the amalgam and is advantageously selected from the group consisting of pure iron, carbon steels, preferably with a carbon content below 0.1 %, nickel and cobalt.
  • the wettability reduces the electrical contact resistance between the amalgam droplets 23 and the internal surface and optionally the uncoated portion of the external surface of the rings.
  • the coating 26 applied to the external surface is conversely non wettable, a feature preventing the adhesion of the amalgam droplets thereby ensuring an easy access of water to the catalytic surface.
  • the overall reaction involves the ionisation of sodium released in the aqueous phase in form of Na + by the amalgam droplets 23 and the passage of electrons across the metal up to the catalyst-coated surface 26 where they participate to the evolution of hydrogen bubbles 28.
  • the overall reaction involves the ionisation of sodium released in the aqueous phase in form of Na + by the amalgam droplets 23 and the passage of electrons across the metal up to the catalyst-coated surface 26 where they participate to the evolution of hydrogen bubbles 28.
  • stripe 29 presents an uncoated metallic surface facing an equivalent surface 27 in order to increase the possibility of contact with the amalgam droplets.
  • the product hydrogen rises to the upper part of the amalgam decomposer and exits nozzle 31 after separating from the caustic soda 30 discharged at 32.
  • Mercury, which contains only minor traces of residual sodium, is sucked in at 33 by the recycle pump 18 to be sent back to the cell.
  • the catalytic coating according to the invention may comprise a variety of components, provided they are, as previously mentioned, sufficiently active towards hydrogen evolution and not wettable by the amalgam. It was found that such requirements are satisfied at reasonable costs by metal carbides of significant electrical conductivity selected from the group of titanium, zirconium, niobium, tantalum, tungsten and silicon carbides.
  • the preferred method for their application to the filling elements is the flame or plasma spraying of micronised powders easily available in sizes comprised between 10 and 100 ⁇ m at reasonable costs due to their widespread use as anti-wear coatings in the metallurgical industry.
  • the plasma is obtainable with a mixture of hydrogen and nitrogen in a ratio comprised for example between 70:30 and 95:5, fed at a flow-rate of 5 - 20 l/min.
  • the powder carrier gas is nitrogen.
  • the application is carried out at a current of 200 - 600 A and a voltage of 50 - 90 V.
  • the distance between the device 36 and the object to be coated is set between 120 and 300 millimetres.
  • the coating application is advantageously carried out on tubes of suitable diameter, for example made of carbon steel, which are rotated in front of the spraying apparatus until obtaining a predetermined thickness of catalytic material: once completed the application step, the coated tubes are cut into equal portions thereby obtaining cylindrical rings characterised in accordance with the invention by having the external and the internal surface respectively coated and uncoated.
  • the particularly preferred cylindrical ring shape of fig. 2 is obtainable making use of the procedure summarised in fig. 3.
  • Carbon steel tubes of suitable diameter 34 are assembled side by side to form a substantially planar structure 35: a flame or plasma spraying device 36, horizontally and vertically movable parallel to the major plane of the structure 35, is placed in front of the latter.
  • the automated displacement of device 36 permits applying the catalytic coating on tubes 34 in form of sprayed material 37.
  • the cutting gives rise to rings presenting about 50% of the external surface and the whole of the internal surface free of catalytic coating.
  • the uncoated portion corresponds to the whole internal surface of the ring and two lateral external stripes 29 corresponding to the zones of structure 35 inaccessible to the sprayed material 37 due to the contact between adjacent pairs of tubes.
  • This type of cylindrical ring proved optimal for amalgam decomposition probably due to the closeness between amalgam droplets in contact with stripes 29 and catalytically coated surface 26.
  • the tubes were previously sandblasted with grit iron until obtaining a surface roughness of 30-40 ⁇ m, then plunged in 20% hydrochloric acid for about 10 minutes.
  • the coating application was carried out by means of a Plasmatechnik plasma apparatus using AMPERIT 570.3 powder provided by H. C. Starck.
  • the source gas for plasma was a mixture of helium at 1.3 l/min flow-rate and nitrogen at 2.5 l/min flow-rate.
  • the carrier gas for the titanium carbide powder was nitrogen at 6.5 l/min flow-rate.
  • the current was set at about 560 A, the voltage at 62 V, the translation rate of the spraying device 36 at about 12 m/min and the gap between spraying device and structure at 35 ⁇ 150 mm.
  • the application was terminated after the deposition of 50 - 80 g/m 2 titanium carbide.
  • the coated tubes were then cut into rings of 2 cm length obtaining a total of 125.000 pieces of the preferred type illustrated in the detail of fig. 2.
  • the rings were then loaded in the decomposer of a 200 kA industrial cell of 1000 mm diameter, with a 1200 mm filling height for a total of 90.000 rings and an overall height of 2100 mm.
  • the cell-amalgam decomposer system was then started with the following main operative parameters detected after a few hours in stable conditions: • current 200 kA
  • This second experimental phase demonstrates the high efficiency of the filling consisting of a stack of rings provided with amalgam-wettable surfaces and catalyst-coated non-wettable surfaces, wherein such surfaces are macroscopically separated: such a conclusion is demonstrated by the capacity of maintaining a perfectly regular functioning even when the filling was reduced by about 30%, a condition which in the case of a prior art graphite filling would lead to a residual sodium concentration in the mercury at the outlet of the amalgam decomposer of about 0.1%, totally unacceptable for a regular electrolytic operation.
  • the previous description is not intended to limit the invention, which may be used according to different embodiments without departing from the scopes thereof, and whose extent is univocally defined by the appended claims.

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Abstract

The invention relates to an amalgam decomposer for mercury cathode chlor-alkali cells. The amalgam decomposer of the invention contains a filling of carbon steel rings whose external surface is provided with a catalytic coating for amalgam decomposition consisting of one or more electrically conductive metals carbides. The internal surface of the rings is free of catalytic coating and wettable by the amalgam, while the external carbide catalytic coating is not wettable by the amalgam thereby favoring hydrogen evolution.

Description

AMALGAM DECOMPOSER FOR MERCURY CATHODE CELLS FOR ALKALI CHLORIDE ELECTROLYSIS
BACKGROUND OF THE INVENTION
The production of chlorine by electrolysis of alkali chloride solutions is currently carried out by means of three different processes, namely the ion-exchange membrane, the porous diaphragm and the mercury cathode one. In the following, reference will be made, for the sake of simplicity of description, to the electrolysis of sodium chloride solutions, nevertheless the invention equally applies to the electrolysis of other alkali chlorides such as lithium or potassium chloride. The mercury cathode-type electrolysis of sodium chloride solutions (brine in the following), based on a long-known technology, has experienced a continuous improvement in the cell structure (Ullmann's Encyclopaedia of Industrial Chemistry, VCH, Vol. A6, pag. 416) essentially directed to the decrease in the electric energy consumption and to the abatement of mercury emissions to the environment.
The problem of energy consumption reduction was tackled with success by replacing the original graphite anodes with titanium anodes provided with a catalytic coating based on oxides of platinum group metals, particularly effective for chlorine evolution. The activated titanium anodes are also characterised by a long operative lifetime which allowed to substantially reduce the amount of cell shut-downs, quite frequent in the case of the corrodible graphite anodes: since maintenance shut- downs are critical for mercury emissions, the benefit obtained from this standpoint is apparent. A further reduction in mercury leaks was moreover allowed by modifications in the cell design, as disclosed in the co-pending Italian patent application MI2006A000309, and by the routinary use of recrystallised salt which permits minimising the quantity of mercury-polluted muds purged from the brine purification section, although at a higher cost. As a consequence of these provisions it can be nowadays demonstrated that the release of mercury from a well-designed and correctly handled plant amounts to no more than 3 grammes per tonne of product chlorine versus a value of 10 grammes of about ten years ago (Ullmann's Encyclopaedia of Industrial Chemistry, VCH, Vol. A6, page 424).
In currently operating plants, the sodium amalgam is fed to the upper portion of an amalgam decomposer shaped as a generally vertical vessel containing a filling of graphite fragments activated with a catalyst, for instance molybdenum oxide. The amalgam flowing down the interstices between the graphite particles meets a countercurrent deionised water flow fed to the lower portion of the amalgam decomposer. The catalytic action of graphite allows the amalgam decomposition reaction to proceed at an acceptable rate, with formation of caustic soda, which together with chlorine is the product of commercial interest, according to the following scheme:
Na(Hg)x + H2O → NaOH + 1/2 H2
In reality the mechanism accounting for the overall reaction is remarkably more complex as it involves the amalgam droplet - graphite particle couples statistically generated in time. Each of these couples actually operates as a short-circuited micro-battery, wherein the amalgam droplet and the graphite particle respectively act as anodic and cathodic area according to the following partial reactions, whose combination gives the above indicated overall reaction:
amalgam droplet (anodic area): Na(Hg)x → Na+ + x Hg + e graphite particle (cathodic area): H2O + e → Y2 H2 + OH"
To obtain a high amalgam decomposition rate it is necessary that the hydrogen evolution partial reaction, which is the bottleneck of the overall kinetics, be adequately promoted. For this reason graphite, which has a moderate activity, is further added with more catalytic materials such as molybdenum oxide which is deposited by imbibition of an ammonium molybdate solution followed by a suitable thermal treatment. The so treated graphite is not wettable by the amalgam: such feature has the advantage of impeding the formation of an adherent amalgam superficial film, that would prevent the required contact with water which is the first step of the hydrogen evolution reaction. On the other hand, this has also a negative effect, because the lack of wettability entails a high electrical contact resistance between graphite particle and amalgam droplet, in its turn strongly hindering the flow of electrons generated by sodium ionisation on the amalgam droplet and that must reach the graphite particle to adequately sustain hydrogen evolution. Hence it is shown that graphite cannot be an optimal catalyst, and this also applies for other homogeneous type formulations, such as the one disclosed in US 4,161 ,433 wherein decomposition catalysts consisting of metal borides and carbides are proposed. From an ideal standpoint in fact any single particle of catalytic material should comprise one or more pairs of separate anodic and cathodic microscopic areas, the anodic ones being wettable by the amalgam and the cathodic ones being non wettable and in intimate contact with the water flow. It would be further necessary to minimise the electrical resistance between the two types of area to provide the lesser hindrance to the electrons flowing from the anodic areas, where they are released by sodium ionisation, to the cathodic areas where they are consumed in the hydrogen evolution reaction.
Besides the above mentioned inconveniences, the graphite particles undergo some grinding under the erosive action of the evolved hydrogen: as a first consequence, the filling undergoes a volume contraction in time that, once a value of about 20% is reached, leads to an intolerable productive capacity loss forcing the operators to discontinue the operation and to proceed with loading fresh catalyst.
From the above discussion it will be clear that the use of activated graphite represents a far from satisfying solution.
The present invention has the purpose of overcoming the drawbacks of the prior art, in particular by providing a novel filling for amalgam decomposers operating in association with mercury cathode-type alkali chloride electrolysis cells. DESCRIPTION OF THE INVENTION
Under a first aspect, the invention relates to a catalyst consisting of amalgam- wettable metallic elements, whose surface is partially provided with a non-wettable catalytic coating, usable as filler for amalgam decomposers.
The elements of the invention are preferably cylindrical rings and the relevant surface partially or completely provided with a non-wettable catalytic coating is the external surface.
The amalgam-wettable metal may be advantageously selected from the group of iron, nickel, carbon steel, stainless steel, however one skilled in the art will also be capable of selecting additional metallic materials with suitable characteristics; according to one preferred embodiment of the invention, the catalytic coating consists of one or more metal carbides selected from the group of titanium, zirconium, niobium, tantalum, tungsten.
The application of the catalytic coating to the surface of the metallic elements may be advantageously carried out by spraying techniques, such as flame or plasma- spraying of powders; the externally coated rings may be manufactured for example by applying the coating through micronised powder spraying on tubes and subsequently sectioning the tubes into rings.
The rings having an external surface partially provided with a catalytic coating may also be manufactured by assembling a multiplicity of tubes in a planar compact structure, applying the catalytic coating by micronised powder spraying on the two major surfaces of the structure and subsequently cutting the structure into rings wherein two lateral stripes of the external surface remain free of catalytic coating.
The invention will be described hereafter making reference to the following explicative drawings: - fig. 1 : device for electrolysis of alkali chloride solutions comprising a mercury cathode cell, the relevant amalgam decomposer and the disamalgamated mercury recycle pump
- fig. 2: sketch of the amalgam decomposer of fig. 1 with a partial internal side- view of the filling consisting of catalytically coated cylindrical rings, with a detail showing the structure of a preferred ring embodiment
- fig. 3: assembly of tubes arranged in a planar compact structure during the spraying of catalytic coating on a major surface thereof
The sketch of fig. 1 represents a longitudinal section of a mercury cathode electrolysis cell with the relevant amalgam decomposer, wherein 1 identifies the cell as a whole, 2 the cell body with the level 3 of brine and with the film 4 of mercury flowing on the carbon steel bottom, 5 the inlet end-box with the outlets 6 and 7 respectively for brine and disamalgamated mercury, 8 the inlet end-box with the outlets 9 and 10 respectively for the depleted brine and for the amalgam generated in the cell, 11 the anodes consisting of a planar structure of titanium rods coated with a catalytic coating for chlorine evolution based on platinum group metal oxides as known in the art, 12 the product chlorine outlet, 13 the amalgam decomposer provided with inlets for the amalgam coming from outlet 10 and for demineralised water 14, and with outlets for caustic soda 15 and hydrogen 16. The anodes and the carbon steel bottom are connected respectively to the positive and to the negative pole of a rectifier (not shown in the figure).
Brine is partially converted to chlorine on the anodes and to sodium amalgam on the mercury mobile film. The depleted brine exiting from 9 is delivered to the dechlorination, resaturation and purification units. The chlorine withdrawn through nozzle 12 is cooled down, dried and pressurised before the direct appliance in user plants or before being liquefied and commercialised. The amalgam produced in cell 1 is decomposed in the amalgam decomposer 13 in which it is put in contact with demineralised water in the catalytic filling 17: the reaction produces concentrated caustic soda, hydrogen and mercury which is recycled to the cell at 7. In the prior art technique the filling 17 consists of graphite particles activated with metal oxides, for instance molybdenum oxide. The conversion of the amalgam to caustic soda and hydrogen must be as complete as possible so that mercury recycled to the cell by pump 18 contains only minimum residual quantities of sodium: due to the poor catalytic capacity of activated graphite, such a result is only obtained by over-sizing the amalgam decomposer. For instance, with cells of average capacity operated with currents of about 200 kA the amalgam decomposer is a cylindrical vessel of about 1100 mm diameter and overall height of 2100 mm, whereof about 1200 mm are occupied by the filling.
The inventors have surprisingly found that the inconveniences of the prior art, consisting of the poor catalytic activity of graphite, the consequent over-sizing of the amalgam decomposer and the insufficient operative lifetime, may be overcome by the introduction of fillings comprising a multiplicity of amalgam-wettable metal elements characterised by having their surface partially coated with a catalytic non amalgam-wettable coating for hydrogen evolution.
The term elements is herein intended to mean portions of metal of various geometrical shapes, dimensioned in order to provide, once stacked to form the filling, an extended contact surface for the reaction between amalgam and water. This object is common to many chemical processes, such as for example the gas absorption in liquid phases or conversely the gas stripping from liquid phases: for such processes, very effective fillings were developed, consisting of a stack of single elements for instance in form of cylindrical rings, cylindrical semi-rings or Raschig rings. The inventors have verified that all of these elements may be advantageously selected for the filling 17: in particular, it was found that the a particularly suitable filling, not only in terms of amalgam decomposition efficiency but also of cost and facility of coating application consists of cylindrical rings with an internal diameter of 10 - 40 mm, thickness of about 1 mm and length comprised between 10 and 40 mm. Fig. 2 shows a more detailed sketch of the amalgam decomposer 13 according to an embodiment of the invention, wherein filling 17 is formed by a stack of cylindrical rings 19 supported by a grid 20. The filling further comprises an element for homogenising the amalgam feed, for instance consisting of a perforated plate 21 also contributing to maintain the rings in position preventing harmful vibrations which could be caused by the evolution of hydrogen. The amalgam, entering from nozzle 22, flows in form of droplets 23 through cylindrical rings 19 in continuous contact with the surfaces thereof. A flow of demineralised water 24 flows countercurrently towards the upper part of the amalgam decomposer, fed through nozzle 25: the water reacts with the amalgam by aid of the catalytic action of rings 19. The structure of a preferred ring embodiment is shown in detail also in fig. 2: the ring 19 has an external surface partially provided with a catalytic coating 26 and an internal surface free of coating 27. The metal of the rings 19 is wettable by the amalgam and is advantageously selected from the group consisting of pure iron, carbon steels, preferably with a carbon content below 0.1 %, nickel and cobalt. The wettability reduces the electrical contact resistance between the amalgam droplets 23 and the internal surface and optionally the uncoated portion of the external surface of the rings. The coating 26 applied to the external surface is conversely non wettable, a feature preventing the adhesion of the amalgam droplets thereby ensuring an easy access of water to the catalytic surface. The overall reaction, as mentioned, involves the ionisation of sodium released in the aqueous phase in form of Na+ by the amalgam droplets 23 and the passage of electrons across the metal up to the catalyst-coated surface 26 where they participate to the evolution of hydrogen bubbles 28. In the preferred ring embodiment in the detail of fig. 2 the external surface is coated only in part with the catalyst: for instance, stripe 29 presents an uncoated metallic surface facing an equivalent surface 27 in order to increase the possibility of contact with the amalgam droplets. The product hydrogen rises to the upper part of the amalgam decomposer and exits nozzle 31 after separating from the caustic soda 30 discharged at 32. Mercury, which contains only minor traces of residual sodium, is sucked in at 33 by the recycle pump 18 to be sent back to the cell.
The catalytic coating according to the invention may comprise a variety of components, provided they are, as previously mentioned, sufficiently active towards hydrogen evolution and not wettable by the amalgam. It was found that such requirements are satisfied at reasonable costs by metal carbides of significant electrical conductivity selected from the group of titanium, zirconium, niobium, tantalum, tungsten and silicon carbides. The preferred method for their application to the filling elements is the flame or plasma spraying of micronised powders easily available in sizes comprised between 10 and 100 μm at reasonable costs due to their widespread use as anti-wear coatings in the metallurgical industry. In particular, details regarding the plasma technology, preferred for the evenness and adherence of the deposited coatings, are disclosed in the brochure "Plasma spray technology, fundamentals and applications, 1975" edited by the Plasma - Technik AG Company, Germany. According to the indications of the brochure, the plasma is obtainable with a mixture of hydrogen and nitrogen in a ratio comprised for example between 70:30 and 95:5, fed at a flow-rate of 5 - 20 l/min. The powder carrier gas is nitrogen. The application is carried out at a current of 200 - 600 A and a voltage of 50 - 90 V. The distance between the device 36 and the object to be coated is set between 120 and 300 millimetres.
When the elements of the filling are cylindrical rings, the coating application is advantageously carried out on tubes of suitable diameter, for example made of carbon steel, which are rotated in front of the spraying apparatus until obtaining a predetermined thickness of catalytic material: once completed the application step, the coated tubes are cut into equal portions thereby obtaining cylindrical rings characterised in accordance with the invention by having the external and the internal surface respectively coated and uncoated. The particularly preferred cylindrical ring shape of fig. 2 is obtainable making use of the procedure summarised in fig. 3. Carbon steel tubes of suitable diameter 34 are assembled side by side to form a substantially planar structure 35: a flame or plasma spraying device 36, horizontally and vertically movable parallel to the major plane of the structure 35, is placed in front of the latter. The automated displacement of device 36 permits applying the catalytic coating on tubes 34 in form of sprayed material 37. When the application is carried out on a single face of structure 35, the cutting gives rise to rings presenting about 50% of the external surface and the whole of the internal surface free of catalytic coating. In any case it was found that the best results are obtained with the type of ring shown in fig. 3 obtained by cutting the tubes after carrying out the application of the catalytic coating on both faces of structure 35: in this case the uncoated portion corresponds to the whole internal surface of the ring and two lateral external stripes 29 corresponding to the zones of structure 35 inaccessible to the sprayed material 37 due to the contact between adjacent pairs of tubes. This type of cylindrical ring proved optimal for amalgam decomposition probably due to the closeness between amalgam droplets in contact with stripes 29 and catalytically coated surface 26.
One of the many experimental tests carried out by the inventors is reported hereafter as a non limiting example.
Assemblies of 50 pieces of Fe 410.2-type carbon steel tube having a length of 1 metre, an internal diameter of 20 mm and a thickness of 1 mm, arranged in mutual contact with one another to form a planar structure of the type indicated as 35 in fig. 3 with an overall size of 1 m x 1 m, were subjected to the application of a catalytic coating consisting of titanium carbide. The tubes were previously sandblasted with grit iron until obtaining a surface roughness of 30-40 μm, then plunged in 20% hydrochloric acid for about 10 minutes. The coating application was carried out by means of a Plasmatechnik plasma apparatus using AMPERIT 570.3 powder provided by H. C. Starck. The source gas for plasma was a mixture of helium at 1.3 l/min flow-rate and nitrogen at 2.5 l/min flow-rate. The carrier gas for the titanium carbide powder was nitrogen at 6.5 l/min flow-rate.
The current was set at about 560 A, the voltage at 62 V, the translation rate of the spraying device 36 at about 12 m/min and the gap between spraying device and structure at 35 ÷ 150 mm.
The application was terminated after the deposition of 50 - 80 g/m2 titanium carbide. The coated tubes were then cut into rings of 2 cm length obtaining a total of 125.000 pieces of the preferred type illustrated in the detail of fig. 2.
The rings were then loaded in the decomposer of a 200 kA industrial cell of 1000 mm diameter, with a 1200 mm filling height for a total of 90.000 rings and an overall height of 2100 mm.
The cell-amalgam decomposer system was then started with the following main operative parameters detected after a few hours in stable conditions: • current 200 kA
• cell voltage 4.2 V
• mercury flow-rate 4.2 m3/h
• sodium concentration in the amalgam at cell outlet 0.3%
• sodium concentration at amalgam decomposer outlet 0.004% • caustic soda concentration at amalgam decomposer outlet 49.8% at 1100C
The functioning was protracted for about 6000 additional hours without noticing any significant variation. After this run the cell was stopped and the amalgam decomposer was opened and inspected without detecting any problem: in particular the filling height was substantially the same measured at the start up. Part of the rings were taken away reducing the filling height to just 830 mm. In these new operative conditions the cell was restarted and the operative data were again collected: it was noticed that the functioning of the amalgam decomposer was unchanged, replicating in particular the values of inlet and outlet sodium concentration in the amalgam and of caustic soda concentration previously obtained with the 1200 mm high filling. Furthermore the functioning conditions remained stable for an additional 5700 hours.
This second experimental phase demonstrates the high efficiency of the filling consisting of a stack of rings provided with amalgam-wettable surfaces and catalyst-coated non-wettable surfaces, wherein such surfaces are macroscopically separated: such a conclusion is demonstrated by the capacity of maintaining a perfectly regular functioning even when the filling was reduced by about 30%, a condition which in the case of a prior art graphite filling would lead to a residual sodium concentration in the mercury at the outlet of the amalgam decomposer of about 0.1%, totally unacceptable for a regular electrolytic operation. The previous description is not intended to limit the invention, which may be used according to different embodiments without departing from the scopes thereof, and whose extent is univocally defined by the appended claims.
Throughout the description and claims of the present application, the term "comprise" and variations thereof such as "comprising" and "comprises" are not intended to exclude the presence of other elements or additives.

Claims

1. Amalgam decomposer for mercury cathode-type electrolytic cells comprising a vertical vessel provided with an internal catalytic filling for the decomposing the amalgam generated inside the cell with water, characterised in that the filling comprises a multiplicity of amalgam-wettable metallic elements whose surface is partially provided with a catalytic coating, said catalytic coating being non-wettable by the amalgam.
2. The amalgam decomposer of claim 1 characterised in that said amalgam- wettable metal is selected from the group consisting of pure iron, carbon steel, nickel and cobalt.
3. The amalgam decomposer of claim 2 characterised in that said carbon steel has a carbon content lower than 0.1 %.
4. The amalgam decomposer of the previous claims characterised in that said catalytic coating comprises at least one metal carbide.
5. The amalgam decomposer of claim 4 characterised in that said at least one metal carbide is electrically conductive.
6. The amalgam decomposer of claim 4 or 5 characterised in that said at least one metal carbide is selected from the group consisting of titanium, zirconium, niobium, tantalum, tungsten and silicon carbides.
7. The amalgam decomposer of any one of the previous claims characterised in that said multiplicity of elements comprises cylindrical rings, cylindrical semi-rings or Raschig rings.
8. The amalgam decomposer of claim 7 characterised in that said cylindrical rings have an uncoated internal surface and an external surface provided at least partially with a catalytic coating.
9. The amalgam decomposer of claim 8 characterised in that said external surface comprises two uncoated lateral stripes.
10. The amalgam decomposer of any one of claims 7 to 9 characterised in that said cylindrical rings have diameter and length independently comprised between
10 and 40 millimetres.
11. Process for the manufacturing of said multiplicity of elements of any one of the previous claims comprising the step of applying said catalytic coating to at least part of the surface of said elements by flame or plasma spraying of powders.
12. The process of claim 11 characterised in that said application step of said catalytic coating by spraying is carried out on the external surface of tubes subsequently cut into a multiplicity of rings.
13. The process of claim 11 characterised in that said application step of said catalytic coating by spraying is carried out on at least one external surface of a planar compact structure consisting of an assembly of tubes, said planar structure being subsequently cut into a multiplicity of rings.
EP07728030A 2006-04-12 2007-04-12 Amalgam decomposer for mercury cathode cells for alkali chloride electrolysis Not-in-force EP2007927B1 (en)

Priority Applications (1)

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Applications Claiming Priority (2)

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IT000731A ITMI20060731A1 (en) 2006-04-12 2006-04-12 DEAD BALER FOR MERCURY CATODO CELLS FOR ALKALINE CHLORIDE ELECTROLYSIS
PCT/EP2007/053563 WO2007116094A2 (en) 2006-04-12 2007-04-12 Amalgam decomposer for mercury cathode cells for alkali chloride electrolysis

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US2423351A (en) * 1943-02-01 1947-07-01 Mathieson Alkali Works Inc Apparatus for amalgam decomposition
BE581152A (en) * 1958-07-29
DE1917714A1 (en) * 1968-12-19 1970-09-03 Elektrochemisches Kom Bitterfe Acceleration of decomposition of sodium-ama- - lgam from electrolytic cells using wc
US3606359A (en) * 1969-08-08 1971-09-20 Ramsey Corp Tungsten carbide coated piston rings
SU385911A1 (en) * 1970-07-27 1973-06-14 METHOD OF ACTIVATING AN ENCLOSURE FOR DECOMPOSITION OF AMALGS
SU431107A1 (en) * 1970-07-27 1974-06-05 В. Н. Антонов, Л. И. Антропов, М. Н. Вайнштейн, Ю. П. Гейд, А. Ю. Ноэль, В. Г. Приходченко, Г. В. Самсонов , А. П. Эпик METHOD FOR PREPARING AN ADDITION FOR DECOMPOSITION OF ALKALI METALS TO AMALHAMS
US3981490A (en) * 1973-05-11 1976-09-21 Vyzkumny Ustav Anorganicke Chemie Apparatus for decomposing alkali metal amalgams
US3875039A (en) * 1974-05-29 1975-04-01 Vyzk Ustav Anorgan Chem Apparatus for decomposing amalgams
IT1113803B (en) * 1977-12-05 1986-01-27 Oronzio De Nora Impianti NEW CATALYTIC MATERIALS FOR THE DECOMPOSITION OF AMALGAMS OF ALKALINE METALS
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